CN101260032B - Modified technique for preparing acrylic acid by propylene two-step oxygenation method - Google Patents
Modified technique for preparing acrylic acid by propylene two-step oxygenation method Download PDFInfo
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- CN101260032B CN101260032B CN2008100503541A CN200810050354A CN101260032B CN 101260032 B CN101260032 B CN 101260032B CN 2008100503541 A CN2008100503541 A CN 2008100503541A CN 200810050354 A CN200810050354 A CN 200810050354A CN 101260032 B CN101260032 B CN 101260032B
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- propylene
- acrylic acid
- wastewater
- acid
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- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 title claims abstract description 63
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 52
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000006213 oxygenation reaction Methods 0.000 title claims description 11
- 238000005406 washing Methods 0.000 claims abstract description 29
- 239000002351 wastewater Substances 0.000 claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 230000003647 oxidation Effects 0.000 claims abstract description 14
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 14
- 239000002253 acid Substances 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 239000002994 raw material Substances 0.000 claims abstract description 6
- 239000000376 reactant Substances 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 21
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 claims description 16
- 230000001590 oxidative effect Effects 0.000 claims description 6
- 241000282326 Felis catus Species 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 239000012943 hotmelt Substances 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- QVKOLZOAOSNSHQ-UHFFFAOYSA-N prop-1-ene;prop-2-enoic acid Chemical group CC=C.OC(=O)C=C QVKOLZOAOSNSHQ-UHFFFAOYSA-N 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 230000008569 process Effects 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 2
- 230000006872 improvement Effects 0.000 abstract description 2
- 238000007670 refining Methods 0.000 abstract description 2
- 239000000203 mixture Substances 0.000 abstract 2
- 238000004880 explosion Methods 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 238000005842 biochemical reaction Methods 0.000 description 1
- 125000003178 carboxy group Chemical group [H]OC(*)=O 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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Abstract
The invention discloses an improved process of preparing acrylic acid through a propylene two-step method, which is characterized in that: the amount of propylene in raw material ratio is increased to ensure that the feed concentration of propylene is 8.0-9.88 percent (mol); washing liquid entering from the top of a washing tower is the mixture of desalted water and acrylic acid containing wastewater; the acrylic acid wastewater is the acid containing wastewater produced by an acrylic acid refining unit in an acrylic acid device; the quantity of wastewater accounts for 50-60 percent (wt) of the total amount of the washing liquid. The improvement has the advantages that: the adoption of high concentration propylene feed can raise the conversion rate of propylene as well as the yield coefficient of acrylic acid, regulate the operating point of oxidation reactant to be beyond the range of an explosion curve, ensure that the device operates in an optimal safe region, reduce the consumption of propylene raw material and raise the production capacity of the device; the adoption of the mixture of desalted water and acrylic acid containing wastewater reduces the dosage of desalted water, the treatment load of a wastewater unit of the device as well as the wastewater discharge amount of the device, and can recycle acrylic acid to the utmost extent, so as to decrease the production cost of the acrylic acid device.
Description
Technical field
The present invention relates to a kind of vinylformic acid preparation technology.
Technical background
Propylene two-step oxygenation legal system vinylformic acid mainly is to be raw material with propylene, air, and the condition that exists at catalyzer issues biochemical reaction, and the first step is that propylene oxidation generates propenal, and second step was that acrolein oxidation generates vinylformic acid, and reaction equation is as follows:
CH
2＝CH-CH
3+O
2→CH
2＝CH-CHO+H
2O
CH
2＝CH-CHO+1/2O
2→CH
2＝CH-COOH
This process is the strong oxidizing reaction of heat release, and temperature of reaction is higher, and when adopting the recycled offgas method, the propylene feed concentration of existing apparatus is less than or equal to 8% (mol), and the propylene consumption is big, and transformation efficiency is low; Simultaneously in the process unit that adopts the recycled offgas method, because scrubber overhead tail gas direct cycles to reactor, therefore oxide catalyst is formed top of tower tail gas higher requirement, the existing apparatus scrubber overhead all adopts the direct absorbing propenoic acid gas of de-salted water to guarantee assimilation effect, to satisfy the catalyzer requirement, therefore to consume a large amount of de-salted waters at production equipment, thereby increase production cost.
Summary of the invention
The objective of the invention is to overcome the deficiency of prior art, a kind of modified technique for preparing acrylic acid by propylene two-step oxygenation method is provided.
Modified technique for preparing acrylic acid by propylene two-step oxygenation method, fresh air, steam, recycled offgas advance premixer M-1001 in the acrylic acid propylene oxidation unit of propylene two-step oxygenation legal system, enter mixing tank M-1002 with propylene again, carry out thorough mixing, charging as the first reactor R-1001, under the catalyzer existence condition, in the first reactor R-1001, propylene and airborne oxygen carry out chemical reaction, generate propenal and a small amount of vinylformic acid, the reaction liberated heat is taken out of by the hot melt salt medium, is used for producing steam; The first reactor R-1001 exit gas mixes in mixing tank M-1003 with additional fresh air, enters the second reactor R-1002, proceeds chemical reaction, makes acrolein oxidation, generates vinylformic acid; The second reactor R-1002 exit gas is through reactant water cooler E-1001 cooling, and cooled propylene acid gas enters washing tower T-1001 bottom, washs absorption, make crude acrylic acid solution, crude acrylic acid is flowed out by washing tower T-1001 bottom, enters next unit, makes with extra care.Washing tower T-1001 top emits tail gas, a part is sent into the catalytic burning unit, another part is through water trap V-1007, carry out processed, tail gas after the dehydration compresses through recycle gas compressor K-1002, recycled offgas after the compression enters premixer M-1001, continues to participate in oxidizing reaction, the invention is characterized in:
A. strengthen the quantity of propylene in proportioning raw materials, making propylene feed concentration is 8.0%～9.88% (mol);
B. the washings that enters of washing tower T-1001 cat head is de-salted water and contains the acrylic acid waste water mixed liquid, and this acrylic acid wastewater be the acid-bearing wastewater of vinylformic acid refined unit generation in this acroleic acid device, and wastewater flow rate accounts for 50%～60% (wt) of washings total amount.
The advantage of this improvement technology:
1. in oxidation reactor charging proportioning is formed, adopt 8.0%～9.88% (mol) high density propylene feed.The high density propylene feed can improve propylene conversion and acrylic acid yield, and its transformation efficiency reaches as high as 97.10%, and yield is up to 87.11%; Adopt high density propylene and low water proportioning charging, do not increase equipment, the operating point that can guarantee oxidation reactant again is outside the blast curve ranges, make device in the operation of the safety zone of the best, reduce propylene feedstocks consumption, reduce the steam consumption of vinylformic acid refined unit, thereby reduce the vinylformic acid production cost greatly.
2. washing tower T-1001 cat head washings, adopt de-salted water and the mixed solution that contains acrylic acid wastewater, adopt pure de-salted water to do the washings contrast with existing apparatus, saved the de-salted water consumption, alleviated waste water unit and handled load, reduced the device wastewater discharge, again acrylic acid to greatest extent, improve the vinylformic acid yield, thereby reduce production costs.
Description of drawings
Accompanying drawing 1 is the concise and to the point process flow sheet of the present invention.
Embodiment
Below in conjunction with specific examples the present invention is made detailed description further.
Fresh air, steam, recycled offgas advance premixer M-1001 in the acrylic acid propylene oxidation unit of propylene two-step oxygenation legal system, enter mixing tank M-1002 with propylene again, carry out thorough mixing, as the charging of the first reactor R-1001, under the catalyzer existence condition, in the first reactor R-1001, propylene and airborne oxygen carry out chemical reaction, generate propenal and a small amount of vinylformic acid, the reaction liberated heat, take out of by the hot melt salt medium, be used for producing steam; The first reactor R-1001 exit gas mixes in mixing tank M-1003 with additional fresh air, enters the second reactor R-1002, proceeds chemical reaction, makes acrolein oxidation, generates vinylformic acid; The second reactor R-1002 exit gas is through reactant water cooler E-1001 cooling, and cooled propylene acid gas enters washing tower T-1001 bottom, washs absorption, make crude acrylic acid solution, crude acrylic acid is flowed out by washing tower T-1001 bottom, enters next unit, makes with extra care.Washing tower T-1001 top emits tail gas, a part is sent into the catalytic burning unit, another part is through water trap V-1007, carry out processed, tail gas after the dehydration compresses through recycle gas compressor K-1002, recycled offgas after the compression enters premixer M-1001, continues to participate in oxidizing reaction, the invention is characterized in:
A. strengthen the quantity of propylene in proportioning raw materials, making propylene feed concentration is 8.0%～9.88% (mol);
B. the washings that enters of washing tower T-1001 cat head is de-salted water and contains the acrylic acid waste water mixed liquid, and this acrylic acid wastewater be the acid-bearing wastewater of vinylformic acid refined unit generation in this acroleic acid device, and wastewater flow rate accounts for 50%～60% (wt) of washings total amount.
1, feature A embodiment
In the acroleic acid device of present domestic operation, adopt in " recycled offgas " legal system acroleic acid device, under the requirement and constraint of catalyzer condition, its propylene feed concentration all is less than or equal to 8% (mol), has caused high material-consumption, makes the cost of device higher.Learn through overtesting with in the actual device service data, in the oxidizing process route plan that two-step oxygenation, recycled offgas directly return, adopt high density propylene, low water proportioning charging, can improve propylene conversion and acrylic acid yield, concrete temperature of reaction data see Table 1-1
The table 1-1 first oxidation reactor temperature of reaction
The table 1-2 second oxidation reactor temperature of reaction
With table 1-2, the contrast of different concns propylene feed process data sees Table 1-3.
Table 1-3 different concns propylene feed data contrast table
With 40,000 tons of acroleic acid devices of annual production is example, and the Technology that adopts two-step oxygenation, recycled offgas directly to return is produced vinylformic acid, and the input concentration of propylene is 8.0% (mol), 2.8 ten thousand tons of year consumption propylene; By technical optimization, the input concentration of propylene is brought up to 9.88% (mol), total recovery brings up to 87.11% by original 85.0%, and the consumption of propylene year is 2.75 ten thousand tons, year saves 2138 tons of refining vinylformic acid steam consumptions.By 10,000 yuan of calculating of propylene per ton, 83 yuan of meters of steam per ton, about 5,000,000 yuan of year saving cost.Therefore, can bring remarkable economic efficiency, see Table 1-4 by improving propylene feed concentration.
Table 1-4 different concns propylene feed device economic efficiency contrast table
Correlation data when adopting the oxidizing process technology of high density propylene feed, can significantly reduce cost, for the user brings remarkable economic efficiency as can be seen from table 1-4.
2, feature B embodiment
With 80,000 tons of/year acroleic acid devices is example, and vinylformic acid oxidation unit scrubber overhead washings adopts de-salted water and de-salted water respectively and contains the acrylic acid waste water mixed liquid and absorbs, and every contrast index sees Table 1-5.The data that provide of table 1-5 are to contain 55% o'clock the situation that the acrylic acid waste water yield accounts for the washings total amount, change not quite when the acrylic acid waste water yield accounts for 50% or 60% situation of washings total amount when containing, and data are close substantially.
Table 1-5 adopts the every technic index contrast table of different sorts washings
From table 1-5, as can be seen, adopt de-salted water and acid-bearing wastewater, annual cost-saved 2,200,000 yuan, bring considerable economic to the user as washings.
Claims (1)
1. modified technique for preparing acrylic acid by propylene two-step oxygenation method, fresh air, steam, recycled offgas advance premixer M-1001 in the acrylic acid propylene oxidation unit of propylene two-step oxygenation legal system, enter mixing tank M-1002 with propylene again, carry out thorough mixing, charging as the first reactor R-1001, under the condition that catalyzer exists, in the first reactor R-1001, propylene and airborne oxygen carry out chemical reaction, generate propenal and a small amount of vinylformic acid, the reaction liberated heat is taken out of by the hot melt salt medium, is used for producing steam; The first reactor R-1001 exit gas mixes in mixing tank M-1003 with additional fresh air, enters the second reactor R-1002, proceeds chemical reaction, makes acrolein oxidation, generates vinylformic acid; The second reactor R-1002 exit gas is through reactant water cooler E-1001 cooling, and cooled propylene acid gas enters washing tower T-1001 bottom, washs absorption, make crude acrylic acid solution, crude acrylic acid is flowed out by washing tower T-1001 bottom, enters next unit, makes with extra care; Washing tower T-1001 top emits tail gas, a part is sent into the catalytic burning unit, another part is through water trap V-1007, carry out processed, tail gas after the dehydration compresses through recycle gas compressor K-1002, recycled offgas after the compression enters premixer M-1001, continues to participate in oxidizing reaction, the invention is characterized in:
A. strengthen the quantity of propylene in proportioning raw materials, making the propylene feed molar percentage is 8.0%～9.88%;
B. the washings that enters of washing tower T-1001 cat head is de-salted water and contains the acrylic acid waste water mixed liquid, and this acrylic acid wastewater be the acid-bearing wastewater of vinylformic acid refined unit generation in this acroleic acid device, and wastewater flow rate accounts for 50%～60% of washings gross weight.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100503541A CN101260032B (en) | 2008-01-27 | 2008-01-27 | Modified technique for preparing acrylic acid by propylene two-step oxygenation method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100503541A CN101260032B (en) | 2008-01-27 | 2008-01-27 | Modified technique for preparing acrylic acid by propylene two-step oxygenation method |
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| CN101260032A CN101260032A (en) | 2008-09-10 |
| CN101260032B true CN101260032B (en) | 2010-09-29 |
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Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101445448B (en) * | 2009-01-01 | 2011-10-26 | 中石油东北炼化工程有限公司吉林设计院 | A energy optimize utilizing process of acroleic acid device reaction unit |
| CN101584969B (en) * | 2009-06-23 | 2012-08-29 | 中石油东北炼化工程有限公司吉林设计院 | Mixer for preparing acrylic acid through propylene two-step oxygenation method |
| CN103193618B (en) * | 2013-03-20 | 2015-11-25 | 中国石油集团东北炼化工程有限公司吉林设计院 | Vinylformic acid washing improving technique in the production of propane single stage method vinylformic acid |
| CN110551008B (en) * | 2018-05-30 | 2022-07-19 | 中石油吉林化工工程有限公司 | Tail gas recycling method in acrolein production process |
| CN110132700B (en) * | 2019-05-27 | 2022-08-02 | 万华化学集团股份有限公司 | Device and process for removing acrolein, acrylic acid and water in gas inlet of on-line propylene infrared analyzer |
| CN112439300A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Tail gas treatment system and tail gas treatment method for preparing acrylic acid |
| CN112441905A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Process for preparing acrylic acid by propylene oxidation |
| CN111138266B (en) * | 2019-11-18 | 2023-07-14 | 中国寰球工程有限公司 | Method and device for preparing acrylic acid or methacrylic acid |
| CN111116335B (en) * | 2019-11-25 | 2023-05-23 | 中国寰球工程有限公司 | Process for the preparation of acrolein or methacrolein |
| CN113636927A (en) * | 2020-04-27 | 2021-11-12 | 兰州金润宏成石油化工科技有限公司 | Pilot plant and process for preparing acrylic acid by propylene oxidation with tail gas circulation |
| CN115974675A (en) * | 2022-08-26 | 2023-04-18 | 中石化宁波工程有限公司 | A high-efficiency and energy-saving reaction system for propylene oxidation to acrylic acid |
| CN116143606A (en) * | 2023-02-27 | 2023-05-23 | 山东兴鲁承宏新材料科技有限公司 | Acrylic acid synthesis process capable of reducing byproducts |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4031135A (en) * | 1974-07-31 | 1977-06-21 | Basf Aktiengesellschaft | Manufacture of acrylic acid by oxidation of propylene with oxygen-containing gases in two separate catalyst stages |
| CN1480441A (en) * | 2002-08-08 | 2004-03-10 | ��ʽ�����ձ���ý | Process for producing acroleic acid |
| CN1572769A (en) * | 2003-06-05 | 2005-02-02 | 株式会社日本触媒 | Method for production of acrylic acid |
| CN1572771A (en) * | 2003-06-05 | 2005-02-02 | 株式会社日本触媒 | Process for producing (meth)acrylic acid |
-
2008
- 2008-01-27 CN CN2008100503541A patent/CN101260032B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4031135A (en) * | 1974-07-31 | 1977-06-21 | Basf Aktiengesellschaft | Manufacture of acrylic acid by oxidation of propylene with oxygen-containing gases in two separate catalyst stages |
| CN1480441A (en) * | 2002-08-08 | 2004-03-10 | ��ʽ�����ձ���ý | Process for producing acroleic acid |
| CN1572769A (en) * | 2003-06-05 | 2005-02-02 | 株式会社日本触媒 | Method for production of acrylic acid |
| CN1572771A (en) * | 2003-06-05 | 2005-02-02 | 株式会社日本触媒 | Process for producing (meth)acrylic acid |
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